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CN104204144A - Process and apparatus for fluid catalytic cracking - Google Patents

Process and apparatus for fluid catalytic cracking Download PDF

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Publication number
CN104204144A
CN104204144A CN201380014273.5A CN201380014273A CN104204144A CN 104204144 A CN104204144 A CN 104204144A CN 201380014273 A CN201380014273 A CN 201380014273A CN 104204144 A CN104204144 A CN 104204144A
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CN
China
Prior art keywords
catalyzer
pipeline
riser reactor
stage
regeneration container
Prior art date
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Granted
Application number
CN201380014273.5A
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Chinese (zh)
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CN104204144B (en
Inventor
P·帕尔马斯
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Honeywell UOP LLC
Universal Oil Products Co
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Universal Oil Products Co
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Publication of CN104204144A publication Critical patent/CN104204144A/en
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C10G11/182—Regeneration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/20—Regeneration or reactivation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/90—Regeneration or reactivation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/06—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using steam
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

One exemplary embodiment can be a process for fluid catalytic cracking. The process can include sending a first catalyst from a first riser reactor and a second catalyst from a second riser reactor to a regeneration vessel having a first stage and a second stage. The first catalyst may be sent to the first stage and the second catalyst may be sent to the second stage of the regeneration vessel. Generally, the first stage is positioned above the second stage.

Description

For the method and apparatus of fluid catalytic cracking
The priority request of early stage national applications
The application requires the U. S. application No.13/425 submitting on March 21st, 2012,657 right of priority.
Invention field
The present invention relates generally to the method and apparatus for fluid catalytic cracking.
Description of Related Art
Catalytic cracking can produce multi-products by larger hydrocarbon.Conventionally, will be compared with heavy hydrocarbon feedstocks, for example vacuum gas oil feeds catalyst cracker as in fluid catalytic cracking reactor.Can produce various products by this system, comprise that gasoline product and/or lighter products are as propylene and/or ethene.
In this system, can use single reaction vessel or double-reactor.Although use two reactor system can cause extra fund cost, one in can operant response device to be suitable for making product as light olefin, comprises the maximized condition of propylene and/or ethene.
In two reactor system, conventionally use valve that catalyzer is sent in riser reactor and revivifier and from riser reactor and revivifier and transmits catalyzer.But the pressure reduction on these valves can change, thereby allow different wear rate.This shortcoming can increase to be safeguarded the shut-down period, and particularly owing to having, the valve of different wear rate causes, and device stops work to allow each valve of displacement conventionally.Therefore, device may be stopped work repeatedly to replace each valve.It is desirable to reduce the standard deviation of pressure reduction on valve or change the wearing and tearing consistence on all valves is provided and reduces and safeguard the shut-down period.
Summary of the invention
A typical embodiments can be fluidized catalytic cracking method.The method can comprise by the first catalyzer from the first riser reactor with from the second catalyzer of the second riser reactor to be sent in the regeneration container with first stage and subordinate phase.The first catalyzer can be sent into first stage and second catalyzer of regeneration container and can send in the subordinate phase of regeneration container.Generally speaking, more than the first stage is positioned at subordinate phase.
Another typical embodiments can be fluid catalytic cracking equipment.This fluid catalytic cracking equipment can have the first riser reactor, the second riser reactor and regeneration container, and described regeneration container is included in the first stage more than subordinate phase.Conventionally, the first riser reactor is sent to spent catalyst in the first stage, and the second riser reactor is sent to spent catalyst in subordinate phase.
Another typical embodiments can be fluidized catalytic cracking method.The method can comprise to be sent into useless the first catalyzer regeneration container from the first riser reactor by the first pipeline, and the first catalyzer of regeneration is sent into the first riser reactor from regeneration container by the second pipeline; With useless the second catalyzer is sent into regeneration container and by the second catalyzer of regeneration and is sent into the second riser reactor from regeneration container by the 4th pipeline from the second riser reactor by the 3rd pipeline.Generally speaking, regeneration container has the first stage more than subordinate phase, and first catalyzer that wherein will give up feeds in the first stage and second catalyzer that will give up feeds in subordinate phase.
Embodiment disclosed herein can be by making useless the second catalyzer move the bottom subordinate phase that is back to regeneration container and reduce pressure change from the first stage.Return owing to reducing useless the second catalyzer, therefore can obtain closer other standpipe head of the pressure reduction of other valve of matching unit.
Definition
As used herein, term " material stream " can be for comprising various hydrocarbon molecules as straight chain, branching or cyclic alkane, alkene, diolefine and alkynes, and optional other mass is if gas is as hydrogen, or impurity is as heavy metal, and the material of sulphur and nitrogen compound flows.Material stream also can comprise aromatics and non-aromatic hydrocarbon.In addition, hydrocarbon molecule can be abbreviated as C 1, C 2, C 3c n, wherein " n " represents the carbonatoms in one or more hydrocarbon molecules.As selection, " material stream " can comprise other gas and replace hydrocarbon molecule, for example oxygen and air.
As used herein, term " district " can refer to comprise the region of one or more equipment parts and/or one or more subregions.Equipment part can comprise one or more reactors or reaction vessel, well heater, interchanger, pipe, pump, compressor and controller.In addition, equipment part can further comprise one or more districts or subregion as reactor, moisture eliminator or container.
As used herein, term " richness " can mean compound in material stream or the amount of a compounds is generally at least 50 % by mole, preferably 70 % by mole.
As used herein, term " substantially " can mean compound in material stream or the amount of a compounds is generally at least 80 % by mole, and preferably 90 % by mole, 99 % by mole best.
As used herein, term " catalyzer " can mean the mixture of single catalyst or catalyzer.In addition, term " the first catalyzer " and " the second catalyzer " can mean catalyzer or the catalyst mixture of same type, the mixture of for example ZSM-5 zeolite and y-type zeolite.Generally speaking, term " the first catalyzer " and " the second catalyzer " refer to position, source or the point of destination of catalyzer, the first riser reactor of for example opposite types and the second riser reactor.
As used herein, term " weight percentage " can be abbreviated as " % by weight ".
As used herein, term " fluid catalytic cracking " can be abbreviated as " FCC ".
As used herein, all pressure disclosed herein is absolute pressure and kPa can be abbreviated as " kPa ".
As used herein, term " riser reactor " means the reactor for fluidized catalytic cracking method conventionally, and it can comprise lifter, reaction vessel and stripper.Conventionally, this reactor can be included in lifter bottom catalyzer is provided, and catalyzer marches to reaction vessel, and reaction vessel has the mechanism that catalyzer is separated with hydrocarbon.
As described in, the technical process line in figure for example refers to pipeline, pipeline, charging, product or material stream interchangeably.
Accompanying drawing summary
Accompanying drawing is the schematic description of a typical stream fluidized catalytic cracking equipment.
Describe in detail
With reference to accompanying drawing, a typical stream fluidized catalytic cracking equipment 100 can comprise the first riser reactor 200, the second riser reactor 300 and regeneration container 400.Generally speaking, the first riser reactor 200 can be included in the first lifter 220 stopping in the first reaction vessel 240.The first lifter 220 can receive the charging 210 of the boiling range can with 180-800 DEG C.Conventionally, charging 210 can be at least one in gas oil, vacuum gas oil, atmospheric gas oil and long residuum.As selection, charging 210 can be at least one in heavy cycle oil and slurry oil.Generally speaking, charging 210 can be for fresh feed, or receives from the recycle stream in product separation district for example with one or more distillation towers.
Generally speaking, charging 210 can provide by any proper height on the first lifter 220, conventionally more than lift gas, provides, and described lift gas provides in the bottom of the first lifter 220.If necessary, charging 210 can provide in the distance that is enough to provide the good distribution that flows up into material and/or catalyzer.Although do not describe, mixing section also can provide in the bottom of the first lifter 220.Typical mixing section is for example disclosed in US 5,451,313.Catalyzer can via pipeline 230 from the second reaction vessel 240 recirculation with improve catalyzer: oil ratio.
Catalyzer can be the mixture of single catalyst or different catalysts.Conventionally, catalyzer comprises two kinds of components, i.e. the first component and second component.This class catalyst mixture is disclosed in for example US7,312,370 and US 2010/0236980 in.
Conventionally, the first component can comprise any catalyzer using in FCC field, for example active amorphous clays type catalyzer and/or high activity, crystalline molecular sieve.Zeolite can be used as molecular sieve in FCC method.Preferably, the first component comprises that large pore zeolite is if y-type zeolite, activated alumina material, adhesive material (comprising silicon-dioxide or aluminum oxide) and inert filler are as kaolin.
Second component can comprise mesopore or the zeolite catalyst of aperture more, for example MFI zeolite, for example, in ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 at least one, and other analogous material.The zeolite of the mesopore that other is suitable or more aperture comprises alkali zeolite and erionite.Second component preferably has the mesopore that is dispersed in matrix or the zeolite of aperture more, and described matrix comprises that adhesive material is if silicon-dioxide or aluminum oxide and inert filler are as kaolin.Second component also can comprise that some other active materials are as beta-zeolite.Preferably first and/or second component at least one be to there is any suitable silicon: the MFI zeolite of aluminum ratio, for example, be greater than 15 silicon: aluminum ratio.
Total mixture in the first riser reactor 200 can comprise 1-25 % by weight second component, in to aperture crystalline zeolite, preferably greater than or equal to 1.75 % by weight second components.The first component can account for the surplus of catalyst composition.
Generally speaking, the first charging 210 and the first catalyzer or catalyst mixture can approach the first lifter 220 bottoms provides.Common the first charging 210 has the temperature of 140-320 DEG C.In addition, also the charging of other amount can be introduced to initial charge point downstream.
In addition, in a desirable embodiment, the first riser reactor 200 can operate under low hydrocarbon partial pressure.Generally speaking, low hydrocarbon partial pressure can promote the preparation of light olefin.Therefore, the first lifter 220 pressure can be 170-450kPa, have 35-180kPa, preferably the hydrocarbon partial pressure of 70-140kPa.Lower hydrocarbon partial pressure can be by using steam or dry gas to realize the hydrocarbon partial pressure that reaches identical as thinner.
One or more hydrocarbon and catalyzer rise in the reaction vessel 240 that transforms the first charging 210.Conventionally, charging 210 in the interior reaction of the first lifter 220 to form one or more products.The first lifter 220 can operate under any suitable temp, conventionally at 150-580 DEG C, preferably at the temperature of 520-580 DEG C, operates.Typical lifter is disclosed in US 5,154,818 and US 4,090,948 in.
Subsequently, catalyzer can be by any suitable device, and the cantilever (swirl arm) 254 for example comprising in shell 250 separates, and falls to the bottom of the first reaction vessel 240.In addition, the first reaction vessel 240 can comprise tripping device, and for example one or more cyclonic separators 258 further to separate product from granules of catalyst.Dipleg (dip leg) can make catalyzer be down to the bottom of the first reaction vessel 240, and its split shed tolerable spent catalyst enters in fine and close catalyst bed.Typical tripping device and cantilever are for example disclosed in US 7,312,370 B2.Catalyzer can pass through stripping zone, and the hydrocarbon absorbing there can be by contacting with steam counter-flow and removing from the surface of this catalyzer.Typical stripping zone is for example disclosed in US 7,312,370 B2.Thereafter, catalyzer can be by being entered in regeneration container 400 and regenerated by pipeline 270.The catalyzer of regeneration can return in lifter 220 via pipeline 280.
One or more products that leave disengaging zone can enter in the ventilating chamber 260 of reaction vessel 240.Conventionally, produce the product that comprises propylene and gasoline.Thereafter, product stream 214 can enter the product separation district for example with one or more distillation towers further to process from the first reaction vessel 240.Zhe Lei district is disclosed in US 3,470, in 084.Conventionally, product separation district can produce several products, for example propylene product and gasoline product.
The second riser reactor 300 that comprises the second lifter 320 and the second reaction vessel 340 can receive charging 310, and described charging 310 can be identical or different with charging 210.In addition, also can use the second catalyzer described above or catalyst mixture.The first catalyzer and the second catalyzer can be identical or different.Conventionally, the second riser reactor 300 can be included in the lifter 320 stopping in reaction vessel 340.
In a preferred embodiment, charging 310 can be one or more C 4-C 10alkene.Charging 310 can be conventionally by fractionation for example further after processing at least in part derived from product stream 214.Conventionally, charging 310 can feed as steam and/or more than light hydrocarbon in the second lifter 320 at lift gas.Generally speaking,, in the time entering in the second lifter 320, the temperature of charging 310 can be 120-600 DEG C.Conventionally, the temperature of charging 310 should be at least more than the boiling point of each component.In addition, charging 310 can directly feed in the second lifter 320, catalyzer have via pipeline 330 from the second reaction vessel 340 recirculation with improve catalyzer: oil ratio.
The second riser reactor 300 can, in temperature, preferably operate at the temperature of 560-620 DEG C.Conventionally can provide the chamber that can receive catalyzer in the second lifter 320 bottoms.This class mixing section is for example disclosed in US 5,451,313.
Generally speaking, the second reaction vessel 340 can comprise catalyzer, preferably ZSM-5 zeolite, and optionally other catalyzer, preferably y-type zeolite.Ideally, the catalyzer in the second reaction vessel 340 is the catalyzer of same type in the first reaction vessel 240.
The second lifter 320 can be with any suitable conditional operation, for example temperature of 425-705 DEG C, the preferably temperature of 560-620 DEG C, and the pressure of 170-450kPa, the preferably pressure of 200-250kPa.Conventionally, the residence time of the second lifter 320 can be less than 4 seconds, is preferably less than 3.5 seconds.Typical lifter and/or operational condition are disclosed in for example US 2008/0035527 A1 and US 7,261, in 807B2.
Generally speaking, charging 310 and catalyzer can rise in the second reaction vessel 340, and catalyzer can use any suitable device to separate with hydrocarbon product, for example cantilever 354.Product hydrocarbon can be in the interior rising of shell 350, and enters in ventilating chamber 360.Thereafter, product can be used as the product stream 314 that comprises ethene and/or propylene and leaves.Granules of catalyst and some hydrocarbon can enter at least one cyclonic separator 358 to separate further to catalyzer and hydrocarbon.Granules of catalyst is down on the fine and close catalyst bed in the second reaction vessel 340.
The second catalyzer can directly feed in stripping zone and through the stripping of material feeding stream and regeneration subsequently as mentioned above.Spent catalyst can feed in regeneration container 400 and via pipeline 380 and return via pipeline 370.
Regeneration container 400 can comprise first stage 420 and the subordinate phase 440 separated by wall or spacer 430.First stage 420 can comprise one or more cyclonic separators 450, can comprise one group of two stage cyclonic separator 450 in this typical embodiments, but can use any suitable quantity.Regeneration container 400 can receive the airflow 404 that approaches subordinate phase 440, and described airflow 404 can comprise the catalyzer of regeneration.Generally speaking, subordinate phase 440 can operate with excessive oxygen, and Poor oxygen gas can upwards enter in the first stage 420 by the pipeline 432 being covered by block 434 separately.Other air can be fed in the first stage 420.First stage 420 operates under partial combustion condition, and wherein flue gas stream 460 leaves the top of regeneration container 400.Catalyzer can be by comprising valve 448 outer catheter 438 leave to be received subordinate phase 440 from the first stage 420.Thereafter, the catalyzer of regeneration can feed in the first lifter 220 by pipeline 280, and feeds in the second lifter 320 via pipeline 380.
Regeneration container 400 can in any suitable condition, for example, operate under the pressure of the temperature of 600-800 DEG C and 160-650kPa.Other typical regeneration container is disclosed in for example US 7,312, in 370B2 and US 7,247,233 B1.
Mention that catalyzer neutralizes the transmission from regeneration container 400 to regeneration container 400, pipeline 270 can be described as the first pipeline 270, and pipeline 280 can be described as the second pipeline 280, and pipeline 370 can be described as the 3rd pipeline 370, and pipeline 380 can be described as the 4th pipeline 380.Generally speaking, the first pipeline 270 and the 3rd pipeline 370 are communicated with to provide spent catalyst with the first reaction vessel 240 and the second reaction vessel 340 stripping zone separately respectively.Conventionally, the first pipeline 270 feeds catalyzer in the first stage 420, and the 3rd pipeline 370 feeds catalyzer in the subordinate phase 440 of regeneration container 400.The second pipeline 280 and the 4th pipeline 380 are communicated with catalyzer to be fed in each lifter 220 and 320 so that the catalyzer of regeneration to be provided with subordinate phase 440.Common each pipeline 270,280,370 and 380 comprises valve 274,284,374 and 384 separately.
Generally speaking, each valve 274,284,374 and 384 has the statical head that produces the pressure reduction on valve.As an example, valve 274 can have the pressure of 300-350kPa on the first riser reactor 200 or upstream side and the pressure of 250-300kPa on regeneration container 400 or downstream side.Similarly, valve 284 can have the pressure of 350-400kPa on regeneration container 400 or upstream side and the pressure of 300-350kPa on the first riser reactor 200 or downstream side.Equally, valve 374 can have the pressure of 400-450kPa on the second riser reactor 300 or upstream side, and on regeneration container 400 or downstream side the pressure of 300-350kPa; And valve 384 can have the pressure of 350-400kPa on regeneration container 400 or upstream side and the pressure of 250-300kPa on the second reactor lifter 300 or downstream side.Conventionally, the pressure difference compared with other valve minimizes each valve 274,284,374 with 384, so the standard deviation of the pressure reduction on all four valves minimizes.
Conventionally, the outlet 378 of pipeline 370 can approach the entrance 382 of the pipeline 380 of the subordinate phase 440 that is positioned at regeneration container 400.Although only determined respectively outlet 378 and the entrance 382 of pipeline 370 and 380, pipeline 270,280,370 and 380 also has entrance and exit.Because the second riser reactor 300 produces the coke of minimum, feasible is to change and to deliver in subordinate phase 440 from the spent catalyst of first stage 420.Conventionally, the second riser reactor 300 processing needs the lighter charging of stringent condition more not to prepare product.The standard deviation of the pressure reduction on all four valves 274,284,374 and 384 is not more than 20kPa or 10kPa.
Illustrative embodiment
Following examples are intended to further set forth theme fluid catalytic cracking equipment.These elaborations of embodiment of the present invention are not intended to claim of the present invention to be limited to the specific detail of these embodiment.These embodiment are based on engineering calculation with by the actually operating experience of similar approach.
A typical stream fluidized catalytic cracking equipment can have two riser reactors that are communicated with regeneration container.Especially, two pipelines (jointly comprising valve 1 and 3) can feed the catalyzer from riser reactor stripping zone separately in the first stage of regeneration container.Two pipelines (jointly comprising valve 2 and 4) can feed the regenerated catalyst of the subordinate phase from regeneration container in each lifter of riser reactor.Each pipeline can comprise valve separately.Each riser reactor can have the pressure of 239kPa and regeneration container and have the pressure of 281kPa.Table 1 has been described the pressure on valve:
Table 1
? Upstream pressure (kPa) Downstream pressure (kPa) Poor (kPa)
Valve 1 331 283 48
Valve 2 368 314 54
Valve 3 303 283 20
Valve 4 368 285 83
About the difference of valve 1-4 and be 205kPa, there is the mean value of 51kPa and there is the standard deviation of 26kPa.Standard deviation calculates by following formula:
Σ ( x - x ‾ ) 2 ( n - 1 )
Wherein: x is observed value;
for the mean value of observed value; And
N is the number of observed value.
Another typical stream fluidized catalytic cracking equipment can have two riser reactors that are communicated with regeneration container.Especially, two pipelines can feed the catalyzer from riser reactor stripping zone separately in the first stage and subordinate phase of regeneration container.Two pipelines can feed the regenerated catalyst of the subordinate phase from regeneration container in lifter separately.Each pipeline can have valve separately.This typical stream fluidized catalytic cracking equipment describe is in accompanying drawing.Each riser reactor has the pressure of 239kPa and regeneration container and has the pressure of 281kPa.Table 2 has been described the pressure on valve:
Table 2
? Upstream pressure (kPa) Downstream pressure (kPa) Poor (kPa)
Valve 274 331 283 48
Valve 284 368 314 54
Valve 374 406 330 76
Valve 384 368 285 83
About the difference of valve 274,284,374 and 384 and be 261kPa, there is the mean value of 65kPa, and there is the standard deviation of 17kPa.This reduction of the standard deviation of the pressure reduction on all four valves can cause valve to wear and tear more equably.This can be by making the subordinate phase 440 that moves to regeneration container 400 from the outlet 378 of the pipeline 370 of first stage 420 realize by the pressure head improving on the valve 374 in pipeline 370.Therefore, the pressure head of pipeline 370 can improve by extending more than 374 duct length of valve.This pressure on valve 374 upstream sides improves the pressure reduction that can improve on valve 374 closer to mate the pressure reduction of other three valves 274,284 and 384.Thereby, and must shut down when the wearing and tearing of independent valve on the contrary, can carry out in the single shut-down period maintenance of all four valves.
Do not further describe, believe that those skilled in the art can use previous description, integrated degree ground uses the present invention.Therefore, it is only illustrative that aforementioned preferred specific embodiments is interpreted as, and the rest part of limit publicity content never in any form.
In the preceding article, unless otherwise noted, all temperature are with a DEG C description, and all parts and percentage ratio are weighing scale.
In previous description, those skilled in the art can easily determine principal character of the present invention, and can not depart from its spirit and scope and make various changes and modifications of the present invention so that it is suitable for various uses and condition.

Claims (10)

1. fluidized catalytic cracking method, it comprises:
A) will send in the regeneration container with first stage and subordinate phase from the first catalyzer of the first riser reactor, more than wherein the first stage is positioned at subordinate phase; With
B) the second catalyzer from the second riser reactor is sent in regeneration container, wherein the first catalyzer was sent in the first stage of regeneration container, the second catalyzer is sent in the subordinate phase of regeneration container.
2. according to the process of claim 1 wherein that the first riser reactor operates under the pressure of 170-450kPa.
3. according to the method for claim 1 or 2, wherein the second riser reactor operates under the pressure of 170-450kPa.
4. according to the process of claim 1 wherein that the first and second riser reactors are under essentially identical pressure.
5. according to the method for claim 1 or 2, it further comprises the first pipeline, the second pipeline, the 3rd pipeline and the 4th pipeline, the first catalyzer from the first riser reactor is sent to regeneration container by the first pipeline, the second pipeline is sent to the first riser reactor by the first catalyzer from regeneration container, the second catalyzer from the second riser reactor is sent to regeneration container by the 3rd pipeline, and the 4th pipeline is sent to the second riser reactor by the second catalyzer from regeneration container.
6. according to the method for claim 5, wherein the first pipeline comprises the first valve, and the second pipeline comprises second valve, and the 3rd pipeline comprises the 3rd valve, and the 4th pipeline comprises the 4th valve.
7. according to the method for claim 6, wherein make the standard deviation of the pressure reduction on all four valves minimize.
8. according to the method for claim 7, wherein make the standard deviation of the pressure reduction on all four valves be not more than 20kPa.
9. according to the method for claim 1 or 2, wherein the first stage comprises one or more cyclonic separators.
10. fluid catalytic cracking equipment, it comprises:
A) the first riser reactor;
B) the second riser reactor; With
C) regeneration container, it is included in the first stage more than subordinate phase, and wherein spent catalyst is sent to the first stage by the first riser reactor, and spent catalyst is sent to subordinate phase by the second riser reactor.
CN201380014273.5A 2012-03-21 2013-03-01 Method and apparatus for fluid catalytic cracking Active CN104204144B (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US13/425,657 US8864979B2 (en) 2012-03-21 2012-03-21 Process and apparatus for fluid catalytic cracking
US13/425,657 2012-03-21
PCT/US2013/028497 WO2013142026A1 (en) 2012-03-21 2013-03-01 Process and apparatus for fluid catalytic cracking

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CN104204144A true CN104204144A (en) 2014-12-10
CN104204144B CN104204144B (en) 2016-08-24

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